Apparatus for the recovery of ethylene glycol in the production of polyethylene terephthalate

ABSTRACT

In an apparatus for the recovery of ethylene glycol in a polyethylene terephthalate(PET) production process water accumulating in the esterification reaction is mixed with a process fluid containing 2-methyl-1,3-dioxolane (MDO). The mixing is carried out in a tank upstream of a rectification column. Through the increase in the water content in the fluid, a shift in the reaction equilibrium takes place and consequently a cleavage of the 2-methyl-1,3-dioxolane present into ethylene glycol and acetaldehyde takes place. Following the cleavage reaction, the mixture is fed from the tank into a rectification column, whereby the ethylene glycol produced from the cleavage reaction is returned to the PET production process.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a division of U.S. patent application Ser. No.12/535,732 filed 5 Aug. 2010 and claims the benefit of the priority ofGerman Patent Application DE 10 2009 044 440.5 filed 18 Aug. 2008, thecontents of which are expressly incorporated herein.

FIELD OF THE INVENTION

The present invention relates to an apparatus for the recovery ofethylene glycol in the production of polyethylene terephthalate (PET).More particularly this invention concerns an apparatus for recoveringethylene glycol from spent ethylene glycol (SEG), which accumulates as abyproduct of the polycondensation reaction forming PET. The SEG contains2-methyl-1,3-dioxolane (MDO), in which ethylene glycol is bonded in theform of an acetal.

BACKGROUND OF THE INVENTION

PET is produced via an esterification reaction of the carboxyl groups ofterephthalic acid and the hydroxyl groups of ethylene glycol, whereinwater separates. The process waste water accumulating through theesterification reaction, which in addition to acetaldehyde, i.a.,contains considerable amounts of ethylene glycol, is subjected to arectification (process column) for the purpose of the recovery of theethylene glycol in the sump of the column. The ethylene glycol may theneither be recovered or returned to the process for preparing PET. Inorder to keep the loss of ethylene glycol low, methods according to theprior art as a rule have structurally sophisticated rectificationcolumns with a plurality of plates or packings. A relatively high refluxratio is necessary for a satisfactory separation of the contaminantscontained in the process waste water, which means a substantial powerrequirement. Despite the separation process that is expensive in termsof energy, the partially purified process wastewater obtained is usuallysubsequently guided over a stripper due to its residual content ofacetaldehyde and other volatile organic components before it is fed to awater treatment plant. In the PET production process moreoversubstantial amounts of contaminated ethylene glycol (spent ethyleneglycol, SEG) accumulates as a byproduct of the polycondensationreaction. The SEG comes primarily from the vacuum system and theethylene glycol circuit of prepolycondensation and contains2-methyl-1,3-dioxolane (MDO), in which ethylene glycol is bonded in theform of an acetal. The SEG process flows from the various process stepsof the PET production process are subjected jointly with the processwastewater to a reprocessing in the rectification column (also referredto here as “process column” or “column”) and then fed again to the PETproduction process. The MDO is a low-boiler, which cannot be held backin the process column, i.e., leaves the process column overhead. Most ofthe MDO is then condensed and reaches the process wastewater as acontaminant. A small part of the MDO is emitted via the exhaust air. TheMDO is the actual reason for the relatively high losses of ethyleneglycol in the process column of PET systems.

International patent application WO 1996/035654 discloses a method inwhich the process wastewater from the PET production process after theprocess column (overhead product) is partially condensed andsubsequently subjected to an inert gas stripping of a reverse osmosis. Areconcentration of the ethylene glycol remaining in the partiallypurified process wastewater is thereby carried out through theapplication of a pressure that is greater than the osmotic pressure ofthe reconcentrated solution. The water is thus pressed through themembrane against the tendency towards the osmotic concentrationequilibrium. The permeate comprises pure water, which can be directlydischarged so that a (complex) water treatment plant is no longernecessary. In addition, the method permits higher ethylene glycolconcentrations in the overhead product of the process column, which onthe one hand reduces the thermal energy required for the column and as aresult reduces the coolant required for the subsequent condensation.Furthermore, the number of the column trays required can be reduced. Theretentate (concentrate) from the reverse osmosis is returned to theprocess, wherein a recirculation is provided either into the reactor ordirectly into the process column. Through this method, although therecovery of ethylene glycol by means of reverse osmosis is improvedcompared to conventional methods, the problem of the loss of ethyleneglycol in the form of MDO is neither recognized nor solved.

OBJECTS OF THE INVENTION

An object of the present invention is now to provide an apparatus, whichare suitable for the recovery of ethylene glycol in the production ofPET.

A further object of the invention is to render possible a saving ofinvestment and/or operating costs and at the same time to implement therecovery of ethylene glycol from SEG in an environmentally friendlymanner.

A further object of the invention is to provide a simple, functionalapparatus for ethylene glycol recovery, requiring a low systemexpenditure and providing energy savings, in particular, by providing areduction in the consumption of raw material with a minimal expenditureand by optimizing the ethylene glycol recovery.

Further objects and advantages of the present invention are shown by thefollowing statements.

SUMMARY OF THE INVENTION

According to the invention, the object is attained through a process forrecovering ethylene glycol in the PET production process, wherein thePET production process contains an esterification reaction in whichprocess wastewater is produced, wherein the process waste water issubjected to at least one separation step preferably a rectification, inwhich at least a part of the contaminants present in the processwastewater are separated and thus a partially purified process wasterwater is produced, wherein at least a part of the partially purifiedprocess wastewater is mixed with a fluid containing2-methyl-1,3-dioxolane (MDO) preferably one or more spent ethyleneglycol (SEG) process flows in a container arranged upstream of therectification column, and the MDO present in the mixture produced iscleaved completely or partially into ethylene glycol and acetaldehyde.

In the PET production process during the esterification or condensationreaction of the terephthalic acid with ethylene glycol (process) wateris produced which leaves the esterification and condensation reactorstogether with other substances as exhaust vapor. The cited substances(referred to below as a whole as contaminants) are, i.a., ethyleneglycol, acetic acid and acetaldehyde. They must be recovered for reasonsof economy or removed to comply with environmental regulations. Theprocess waste water, that is the sum of (process) water andcontaminants, is therefore subjected to one or more separation steps,wherein a first separation usually takes place by distillation in arectification column. There most of the ethylene glycol present isseparated, remaining in the sump, and which may then be either recoveredor returned to the PET process, and the overhead product of the columnis subsequently fed to a condenser, wherein a part of the acetaldehydeand other low-boilers remain in the gas phase and are fed as exhaust airto a thermal or catalytic combustion. Through a first separation step ofthis type a partially purified process waste water is produced, whichaccording to previous practice is often also guided over a stripperbefore it is fed into a water treatment plant or is directly ejected aswaste water.

In addition to partially purified process waste water, substantialquantities of contaminated ethylene glycol (spent ethylene glycol, SEG)accumulate in the PET production process, which contains, i.a., MDO. TheSEG comes in particular from the vacuum system and the ethylene glycolcircuit of the prepolycondensation. The SEG process flows from thevarious process steps of the PET production process are often combinedin a collecting tank (SEG tank or SEG collecting tank), subsequentlysubjected to a separation step in a rectification column and then isreturned to the PET production process.

The MDO is a low-boiler which cannot be held back in the rectificationcolumn, i.e., leaves the column overhead together with the (process)water. The large part of the MDO is then condensed together with the(process) water and discharged as part of the partially purified processwastewater. A small part of the MDO is emitted via the exhaust air. Theexistence of the MDO is the actual cause of the relatively high lossesof EG in the column of PET systems. MDO is stable under neutral; andslightly alkaline pH conditions, in the acid range depending on thewater content, preferably at a pH of 3 to 6, MDO decomposes into thestarting materials ethylene glycol and acetaldehyde. The formation aswell as cleavage of the MDO are acid-catalyzed.

It was recognized that the partially purified process waste water (or apart thereof) can be used to increase the water content in ethyleneglycol (SEG) contaminated with MDO from the PET production process tothe extent that by shifting the chemical equilibrium a cleavage of asubstantial part of the MDO present into ethylene glycol andacetaldehyde takes place. An acceleration of the MDO cleavage isrendered possible by feeding acid components in the partially purifiedprocess wastewater. Nevertheless, a certain dwell time for the course ofthe MDO cleavage reaction is necessary. For this reason the partiallypurified process wastewater and the spent glycol are combined in a tankfrom which the rectification column is then fed. The tank provides thenecessary dwell time for the cleavage reaction. Compared to arectification process, which does not provide an upstream MDO cleavage,this thus has the advantage that the reflux ratio in the process columncan be reduced due to the lower MDO content of the exhaust vapor, whichis advantageous for economic reasons. Acetaldehyde is formed as afurther reaction product from the MDO cleavage. This is a low-boilerthat can be fed via process column partially via the gas phase to anexhaust air treatment.

In the present application, a partially purified process wastewatermeans process waste water that has passed through at least oneseparation step. A reprocessing by distillation in a column is providedas a preferred first separation step, wherein the forming partiallypurified process wastewater preferably contains the substances listed intable 1 in the quantities given. As the table shows, the partiallypurified process wastewater also has a significant MDO content.

All of the percentages given here are to be understood as percent byweight unless stated otherwise. The basis is the respectively cited massflow.

The term “process” or “PET production process” or “PET productionmethod” means the entire process for producing PET, including allconversions and substance flows. Accordingly, “system” means the entiresystem for producing PET. Expressions such as “water with:” or “ethyleneglycol with water” (EG with H₂O) refer to the respective main componentsof the material flow, that is, the residual amount after removal of thecontaminants. Preferably these have a content of the main component ofat least 30% by weight, wherein at least 60% by weight and in particular90% by weight are particularly preferred.

The terms “water,” “(process) water” or “process wastewater” do notreveal anything about the state of aggregation. The partially purifiedprocess wastewater can consequently be present not only in liquid form,but also in gaseous form.

TABLE 1 Partially purified process wastewater after process column andcondenser Mass Flow (total)  185-195 kg/t PET H₂O with ethylene glycol 0.4-0.6% 2-methyl-1,3 dioxolane  0.3-0.6% Acetic Acid  0.1-0.2%*0.01-0.02%** 1,4-dioxane 0.04-0.06% Acetaldehyde  0.9-1.5% Temperature  30-40° C. *With the use of antimony acetate as catalyst in the PETproduction process. **With the use of antimony trioxide as catalyst inthe PET production process

It can be advantageous to subject the partially purified processwastewater to one or more further separation steps before the mixingwith SEG, wherein this is preferably a (further) process column and/or astripper. Stripped, partially purified process wastewater preferablycontains the substances listed in Table 2 in the specified amounts.

TABLE 2 Partially purified process wastewater after process column andstripper Mass Flow (total)   170-180 kg/t PET H₂O with EG  0.2-0.6%2-methyl-1,3 dioxolane  0.01-0.05% Acetic Acid  0.06-0.2%* 0.006-0.02%**1,4-dioxane  0.01-0.05% Acetaldehyde  0.01-0.03% Temperature   30-60° C.*With the use of antimony acetate as catalyst in the PET productionprocess. **With the use of antimony trioxide as catalyst in the PETproduction process

The stripping is preferably carried out thereby with air as strip gas.

The above-referenced method according to the invention is particularlyadvantageous if at least a part of the partially purified processwastewater is subjected to at least one reverse osmosis and/orultra/nanofiltration before the mixing with the fluid containing MDO,wherein preferably that part of the process wastewater which accumulateswith the reverse osmosis and/or ultra/nanofiltration as retentate isused at least in part for mixing with the fluid containing2-methyl-1,3-dioxolane.

Various advantages result from a process control of this type. Dependingon the embodiment (single-stage to three-stage), the use of a reverseosmosis makes it possible to omit a (complex) wastewater treatment,since the permeate comprises slightly contaminated to uncontaminatedwater. According to the invention, however, even with the use of reverseosmosis and/or ultra/nanofiltration depending on the embodiment of themembrane methods and the valid environmental regulations a finalwastewater treatment can nevertheless be provided, wherein, however,this can be embodied more simply and operated at less expense due to thepre-treatment of the process wastewater (here: permeate). In addition,the use of a reverse osmosis leads to lower MDO concentrations in theoverhead product of the rectification column, which reduces the thermalenergy needed for the column (reflux) and consequently the coolantrequirement for the subsequent condensation. Furthermore, the number ofcolumn is trays needed can be reduced.

In addition to the referenced advantages, through the method accordingto the invention, i.e., through the cleavage of the MDO, furthermoreethylene glycol can be recovered. The retentate (concentrate) from thereverse osmosis, i.e., the part of the partially purified processwastewater enriched with ethylene glycol, is thereby preferably used toincrease the water content in the SEG. Although the (process) waterreturned to the PET production process, preferably into the column, mustbe evaporated and subsequently condensed, in contrast to the methodaccording to the prior art this disadvantage in terms of energy is morethan compensated for by the recovered ethylene glycol. In contrast tothe prior art, therefore, no minimization of the retentate volume bymeans of reverse osmosis needs to be undertaken. The method according tothe invention therefore makes it possible to keep the pressure—and thusthe energy expenditure—lower during the reverse osmosis. Furthermore, apart of the fed (process) water is used during the cleavage of the MDO.The reverse osmosis and/or ultra/nanofiltration is preferably carriedout at temperatures of 20-50° C. and/or pressures of 5-70 bar(g).

Partially purified, in particular not stripped process wastewatercontains significant quantities of 1,4 dioxane (see Tables 1 and 2).Since 1,4 dioxane is virtually not biologically degradable, thefrequently required low outflow values after water treatment plant withrespect to chemical cumulative parameters such as, e.g., COD (chemicaloxygen demand) and total organic carbon (TOC) are not achieved. With thedescribed application of reverse osmosis and/or ultra/nanofiltration, alarge part of the 1,4 dioxane contained in the process wastewater isreturned to the PET production process and from there is easily treatedvia the exhaust gas in a thermal or catalytic exhaust air purification.The permeate depleted from 1,4 dioxane is fed to a water treatmentplant, wherein with the identical equipment of the water treatment planta clearly improved outflow quality can now be achieved with respect tochemical cumulative parameters such as e.g. COD and TOC.

After running through the reverse osmosis and/or ultra/nanofiltration,the partially purified process wastewater preferably contains thesubstances listed in Table 3 (retentate) and Table 4 (permeate) in theamounts listed

TABLE 3 Partially purified process waste- water/retentate from reverseosmosis. Method with stripper: Mass Flow (total)   4-22 kg/t PET WaterWith: Ethylene glycol   3-10% 2-methyl-1,3 dioxolane  0.1-0.6% AceticAcid  0.5-2%* 0.05-0.2%** 1,4-dioxane  0.1-0.6% Acetaldehyde Notrelevant Temperature   20-40° C. Method without stripper: Mass Flow(total)   4-22 kg/t PET H₂O with EG   3-10% 2-methyl-1,3 dioxolane  3-10% Acetic Acid  0.7-2%* 0.07-0.2%** 1,4-dioxane  0.5-0.8%Acetaldehyde Not relevant Temperature   20-40° C. *With the use ofantimony acetate as catalyst in the PET production process. **With theuse of antimony trioxide as catalyst in the PET production process

TABLE 4 Partially purified process waste- water/permeate from reverseosmosis Method with stripper: Mass Flow (total)   152-170 kg/t PET Waterwith: Ethylene Glycol  0.05-0.15% 2-methyl-1,3 dioxolane ca. 0.005%Acetic Acid  0.05-0.1%* 0.005-0.01%** 1,4-dioxane 0.002-0.006%Acetaldehyde Not relevant Temperature   20-40° C. Method withoutstripper: Mass Flow (total)   168-185.7 kg/t PET H₂O with EG  0.05-0.15%2-methyl-1,3 dioxolane ca. 0.07% Acetic Acid  0.07-0.12%* 0.007-0.012%**1,4-dioxane 0.002-0.006% Acetaldehyde Not relevant Temperature   20-40°C. Discharge as wastewater for final cleaning in a chemical/biologicalwaste water cleaning. *With the use of antimony acetate as catalyst inthe PET production process. **With the use of antimony trioxide ascatalyst in the PET production process

With the use of a reverse osmosis, the retention degrees listed in Table5 below are to be anticipated:

TABLE 5 Retention degrees* of reverse osmosis. Ethylene glycol 75-85%2-methyl-1,3 dioxolane 80-90% Acetic Acid 45-55% 1,4-dioxane 85-95%Acetaldehyde Not relevant *Method with/without stripper

In the present application, SEG process flows are to be understood tomean all process flows contaminated with MDO in the PET productionprocess, which essentially contain ethylene glycol. The SEG or the SEGprocess flows used in the method according to the invention preferablyhave an ethylene glycol content of at least 30% by weight, wherein acontent of at least 60% by weight and in particular at least 90% byweight is particularly preferred. The SEG process flows used accordingto the invention are preferably the material flows which the ethyleneglycol circuit of the prepolycondensation comprises, as well as SEGprocess flows from the vacuum system of the prepolycondensation.

The SEG from the prepolycondensation preferably contains the substanceslisted in Table 6 in the amounts given.

TABLE 6 SEG flow *** from prepolycondensation into SEG collecting tankMass flow   90-110 kg/t Eylene glycol with: Water   3-7 % 2-methyl-1,3dioxolane  0.2-0.7% Acetic Acid  ca. 0.1%* ca. 0.01%** 1,4-dioxane0.02-0.04% Acetaldehyde Not relevant Temperature   35-60°C *With the useof antimony acetate as catalyst in the PET production process **With theuse of antimony trioxide as catalyst in the PET production process***Method with/without stripper

Since the SEG or the SEG process flows are mostly present in liquid formand the process wastewater for treatment in the reverse osmosis unitlikewise has to be available in liquid form, it is preferred to mix SEGand partially purified process wastewater in liquid form. However, amixing is also conceivable in which the SEG as well as the partiallypurified process wastewater are present in gaseous form, or a mixing inwhich one of the components to be mixed is available entirely orpartially in gaseous form, while the other is entirely or partiallyliquid.

According to the present invention, before or during the mixing of theSEG with the partially purified process wastewater preferably acombination of two or more of the SEG process flows of the PETproduction process is provided. An SEG collecting tank such as isalready available in most systems according to the prior art ispreferably used in the combination of the SEG process flows. Inaddition, one or more further tanks can be provided in which the mixingof the SEG with the partially purified process wastewater and theconversion of the MDO take place. However, it is preferred according tothe invention that the mixing likewise takes place in the SEG collectingtank, which to that end i.a. is supplemented with one or more feedconduits for partially purified process wastewater. In this manner anadditional container for the conversion of the MDO is not needed, iswhich reduces the number of system parts necessary, with which areduction of the investment and operating expenditure is achieved.Moreover, mixing elements can be provided which, for example, arelocated either in the tank itself or are arranged as static mixingelements upstream of the tank. Accordingly, instead of separate feedconduits for SEG and partially purified process wastewater, thecontainer can also have one or more feed conduits that supply SEG andpartially purified process wastewater jointly. The (one or more) tank(s)is preferably designed such that at least 20% by weight, preferably atleast 40% by weight of the MDO present in the supplied SEG and/or the

MDO present in the supplied in the partially purified process wastewatercan be cleaved into ethylene glycol and acetaldehyde. Accordingly, acited method for the recovery of ethylene glycol is particularlypreferred when in the (one or more) tank(s) 20-80% by weight, preferably30-70% by weight, particularly preferably 40-60% by weight of the MDOpresent in the supplied SEG and/or in the supplied partially purifiedprocess water is cleaved into ethylene glycol and acetaldehyde or theMDO cleavage rate in the tank achieves these values.

In addition to the above referenced method, the present invention alsoincludes a system for the production of PET with one or moreesterification and/or transesterification reactors as well as one ormore devices for the production of a partially purified processwastewater through the separation of contaminants present in the processwastewater, which preferably is a rectification column, wherein thesystem has one or more tanks, which have at least one feed conduit forpartially purified process wastewater and at least one feed conduit fora fluid containing MDO (preferably an ethylene glycol process flow)and/or one or more feed conduits for a mixture of partially purifiedprocess wastewater and a fluid containing MDO.

A cited system is to be considered particularly advantageous when it hasa reverse osmosis device and/or an ultra/nanofiltration device, which isarranged upstream of the tank in terms of process engineering.

In this case, the system preferably has one or more lines that feedsthat part of the partially purified process wastewater which accumulatesas retentate in the reverse osmosis unit and/or ultra/nanofiltrationunit (or a part thereof) directly or indirectly to the tank. The systemtherefore advantageously has one or more lines that run between thereverse osmosis unit and/or the ultra/nanofiltration unit and the tank.

The inflow of partially purified process wastewater into the tank ispreferably controlled depending on the water content of the mixture inthe tank, which is preferably measured periodically. If a reverseosmosis unit and/or an ultra/nanofiltration unit is provided, thepressure in the reverse osmosis unit and/or ultra/nanofiltration unit orthe degree of the reconcentration can also be controlled depending onthe water content in the tank in order to achieve an increased or lowerenrichment of ethylene glycol and/or acetic acid or a higher or lowerwater content. It can also be advantageous to control the separationpower of the process column depending on the water content in the tank,for example, via the adjustment of the reflux ratio.

A system such as is described above is particularly advantageous whenthe volume of the container is dimensioned such that the dwell time is0.2-4 hours, preferably 0.5-3 hours, particularly preferably 1-2 hours.

In this manner a decomposition of a substantial part of the MDO isensured. The tank serves at the same time as a buffer for SEG and/orpartially purified process wastewater. “Dwell time” means the dwell timeof the contents of the tank, i.e., the mixture of partially purifiedprocess wastewater and SEG.

According to a further preferred embodiment, in the above-mentionedmethod or in the cited system the cleavage of the MDO takes place in thepresence of one or more catalysts, wherein the catalysts are preferablyone or more of the following: “organic aliphatic and aromatic acids,preferably acetic acid.”

A referenced method is in particular advantageous when one or more acidscontained in the process wastewater, preferably acetic acid arereconcentrated (preferably by means of reverse osmosis) and used ascatalysts for the cleavage of the MDO.

This is another reason why the use of a reverse osmosis and/orultra/nanofiltration is favored with the method according to theinvention. Through reverse osmosis and/or ultra/nanofiltration not onlycan a reconcentration of MDO in the process wastewater and a recovery ofethylene glycol be achieved, but also a reconcentration of othercontaminants or ingredients, in particular organic acids such as aceticacid. These are thus kept in the process and can be used, for example,as catalysts in the MDO cleavage. If the amount of catalysts is toosmall, an addition from outside is also conceivable. Preferably thecatalysts are substances that essentially do not negatively affect theother processes connected with PET production and thus can be guided inthe circuit. That means that the catalysts, which are preferably acidcompounds, can be returned to the tank via the partially purifiedprocess wastewater and/or the SEG process flows and thus can acceleratethe MDO cleavage.

The cleavage of the MDO is an equilibrium reaction. Consequently, withthe increase of the water concentration in the mixture, the chemicalequilibrium is shifted in the direction of the MDO cleavage productsethylene glycol and acetaldehyde. Since the water in the process columnmust be evaporated again, it is advantageous to keep the waterproportion in the mixture low. The conversion of the MDO in the tanktherefore preferably occurs under conditions such as are listed in Table7. Thus on the one hand a cleavage of an essential part of the MDO isensured and on the other hand the additional expenditure in connectionwith a return of the water into the process is thus allowed for.

TABLE 7 Conditions for MDO cleavage in the SEG collecting tank* Dwelltime: 0.5-3 h, preferably:   1-2 h Temperature: 35-95° C.,preferably: 40-60° C. Concentration of water: ≧10%, preferably:  15-25%Concentration of acid 0.1-1%, preferably: 0.2-0.4% Exhaust air Dischargesuction of the acetaldehyde formed, Discharge via exhaust air collectorline for thermal or catalytic exhaust air treatment Cleavage rate ofMDO: 20-80-%, preferably: 40 to 60% *Method with/without stripper

As also set forth in Table 7, another possibility for shifting theequilibrium in the direction of the MDO is to suction off acetaldehydefrom the tank. The pressure in the container is thus preferably adjustedsuch and optionally coordinated with the other conditions (cf. Table 7)such that the cleavage rate cited in Table 7 is achieved.

The quantity of recovered ethylene glycol is shown in Table 8.

TABLE 8 Ethylene glycol recovery rate With the use of a process columnand a stripper: General recovery rate of ethylene glycol: By reverseosmosis (RO) 0.3-0.9 kg/t PET By MDO cleavage 0.1-0.5 kg/t PET Thefollowing ethylene glycol recovery rates apply for stripped partiallypurified process wastewater RO + MDO cleavage: 0.5-1.3 kg/t PET Byadjustment of the operating parameters of the existing stripper systemto the reverse osmosis/MDO cleavage, the EG recovery rate can beincreased to at least 1.5 kg/t By using a process column, without theuse of a stripper: General recovery rates of ethylene glycol: By RO0.6-1.0 kg/t PET By MDO cleavage 0.1 to 1.0 kg/t PET The followingethylene glycol recovery rates apply for unstripped partially purifiedprocess wastewater: RO + MDO cleavage 0.8-1.8 kg/t PET

The above-referenced method is particularly important when the mixtureof SEG and partially purified process wastewater has a water content ofat least 10% by weight, preferably 13 to 45% by weight, particularlypreferably 15-25% by weight. Preferably the inflow of SEG and partiallypurified process wastewater to the tank is controlled such that theabove-referenced water content of the mixture is achieved.

If an MDO cleavage rate of approximately 50% is provided, the mixture ofSEG and partially purified process wastewater preferably contains thesubstances listed in Table 9 in the listed quantities. This ispreferably the process flow that is guided back into the PET productionprocess.

TABLE 9 Mixture SEG flow + partially purified processwastewater/retentate after MDO cleavage at 50% Method with stripper:Mass Flow   94-132 kg/t PET Ethylene glycol with water   10-20%2-methyl-1,3 dioxolane  0.2-0.7% Acetic Acid  0.1-0.3%* 0.01-0.03%**1,4-dioxane 0.05-0.08% Acetaldehyde Not relevant Temperature   35-60° C.Method without stripper: Mass Flow   94-132 kg/t PET Ethylene glycolwith water   10-20% 2-methyl-1,3 dioxolane  0.3-0.8% Acetic Acid 0.2-0.4%* 0.02-0.04%** 1,4-dioxane 0.08-0.12% Acetaldehyde Not relevantTemperature   35-60° C. *With the use of antimony acetate as catalyst inthe PET production process. **With the use of antimony trioxide ascatalyst in the PET production process

As mentioned, the return of the partially purified process wastewaterinto the PET production process is carried out in the form of a mixingwith the SEG. In this respect an above-referenced method is particularlyadvantageous when the mixture (completely or in part) after the cleavageof at least part of the MDO is returned to the PET production process atone more points. It is particularly preferred thereby to provide areturn to a process column of the PET polycondensation system and/or anethylene glycol recovery system.

The material flows referenced in the application are mutuallyinterdependent and the decision on how their composition and otherproperties are to be selected depends on the objective that is to beachieved. It was established that material flows that lie in theconcentration ranges with respect to their composition as they are givenin the tables above are preferred. These ensure an MDO conversion ratethat is particularly advantageous with respect to ethylene glycolformation and for economic reasons. However, the invention is notrestricted to the given values.

BRIEF DESCRIPTION OF THE DRAWING

FIG. 1 is a flow diagram showing the process steps, both with andwithout a stripper, which is optional, the elements of the apparatusparts and the material flows that are relevant or preferred for theethylene glycol recovery in the PET production process.

DETAILED DESCRIPTION OF THE DRAWING

In the PET production process during the esterification or condensationreaction of the terephthalic acid with ethylene glycol (process) wateris produced which leaves the esterification reactor 18 together withother substances as exhaust vapor which exits the esterification reactor18 through line 17 for the rectification column 5. The cited substances(referred to below as a whole as contaminants) are, i.a., ethyleneglycol, acetic acid and acetaldehyde. They must be recovered for reasonsof economy or removed to comply with environmental regulations. Theprocess wastewater, that is the sum of (process) water and contaminants,is therefore subjected to one or more separation steps, wherein a firstseparation usually takes place by distillation in the rectificationcolumn 5. There most of the ethylene glycol present is separated,remaining in the sump, and which may then be either recovered orreturned to the PET process (not shown in the drawing), and the overheadproduct of the column is subsequently fed to a condenser 6, wherein apart of the acetaldehyde and other low-boilers remain in the gas phaseand are fed as exhaust air through line 9 to a thermal or catalyticcombustion. Through a first separation step of this type a partiallypurified process wastewater is produced, which is optionally passedthrough a stripper 7 for separating out volatile components before it isfed into a water treatment plant comprising a cooler 11, a line 10 forchanneling the partially purified waste water from the cooler to aprefilter 12, after which the partially purified waste water is passedto a reverse osmosis apparatus 13 comprising an osmotic membraneseparating a chamber for the permeate and a chamber for the retentate.The permeate exits the process through line 15 where it is ready forfinal purification in a chemical-biological waste water treatment.Alternatively the partially purified waste water may be directly ejectedfrom the process as wastewater. The retentate containing the partiallypurified waste water which still includes some MDO not already cleavedby hydrolysis exits the reverse osmosis apparatus through line 14 and ischanneled to the collecting tank 1 where it is mixed with fresh SEG flowfrom line 2 from the various process steps of the PET process.

In addition to partially purified process wastewater, substantialquantities of contaminated ethylene glycol (spent ethylene glycol, SEG)accumulate in the PET production process, which contains, i.a., MDO. TheSEG comes in particular through line 2 leading from the vacuum system 24which communicates with the prepolycondensation reactor 21 throughexhaust line 23. The SEG process flows from the various process steps ofthe PET production process are combined through line 2 in a collectingtank 1 (SEG tank or SEG collecting tank). There the MDO is contactedwith the retentate from the osmosis channeled through line 14 andhydrolyzed at least in part, at an acid pH, preferably 3 to 6, andcleaved into ethylene glycol and acetaldehyde. The mixture comprisingpartially purified process wastewater and ethylene glycol recovered fromMDO through hydrolytic cleavage is then led from the collecting tankthrough line 4 and subsequently subjected to a separation step in therectification column 5, where the ethylene glycol flows to the sump ofthe rectification column and may then be returned to the PET productionprocess (return not shown).

The MDO in the head of the rectification column is a low-boiler whichcannot be held back in the rectification column, i.e., leaves the columnoverhead together with the (process) water. The large part of the MDO isthen condensed together with the (process) water and discharged as partof the partially purified process wastewater, either to the stripper 7or directly through line 16 to the water treatment plant. A small partof the MDO is emitted via the exhaust air 9.

The invention is described below based on examples, wherein theinvention of course is not limited to these illustrated embodiments.

The illustrated embodiments show the composition of the material flowsas they can occur in a system according to the invention for PETproduction with a capacity of 330 t/d. A process column is provided asthe first separation step or as separation device for the processwastewater. Furthermore, an is ethylene glycol enrichment by means ofreverse osmosis takes place.

Abbreviations and Notes:

With respect to the designation of the material flows “Flow [no.]”),reference is made to the process diagram shown in FIG. 1.

The designation “*” means that antimony acetate was used as a catalystin the PET production process, whereas “**” indicates the use ofantimony trioxide as a catalyst in the PET production process.

LIST OF REFERENCE NUMBERS

-   -   1. Tank/SEG collecting tank    -   2. (Flow 2): SEG from prepolycondensation    -   3. (Flow 3): Exhaust air from container    -   4. (Flow 4): SEG+retentate from reverse osmosis    -   5. Process column    -   6. Condenser    -   7. Stripper system    -   8. (Flow 8): Air    -   9. (Flow 9): Total exhaust air for treatment    -   10. (Flow 10): Partially purified process wastewater after        stripper    -   11. Cooler    -   12. Prefilter    -   13. Reverse osmosis unit    -   14. (Flow 14): Partially purified process wastewater/retentate        from reverse osmosis    -   15. (Flow 15): Partially purified process wastewater/permeate        from reverse osmosis    -   16. (Flow 16): Partially purified process wastewater after        process column (alternative embodiment without the use of a        stripper)    -   17. Line (for process wastewater in the form of process exhaust        vapors)    -   18. Esterification reactor    -   19. Paste batch    -   20. Lines (for monomers)    -   21. (Pre)polycondensation reactor    -   22. Line (for polymer)    -   23. Line (for exhaust vapors from the (pre) polycondensation)    -   24. Vacuum device (including condenser)    -   25. Line (for exhaust air)

EXAMPLE 1

The following tables show the material flows in a PET productionprocess, wherein after running through a process column the processwastewater is subjected to another separation step (stripping with air):

Flow 10 (Partially purified process wastewater after stripper)

Mass Flow (total) 2400 kg/h Water with: ethylene glycol  0.4%2-methyl-1,3 dioxolane 0.03% Acetic Acid  0.15%* 1,4-dioxane 0.03%Acetaldehyde Not relevant Temperature 35-45° C.

Flow 14 (Partially purified process wastewater:retentate from reverseosmosis)

Mass Flow (total) 180 kg/h Water with: Ethylene glycol  4.3%2-methyl-1,3 dioxolane 0.35% Acetic Acid     1%* 1,4-dioxane 0.35%Acetaldehyde Not relevant Temperature 30-40° C.

Retention degrees of reverse osmosis:

Ethylene glycol 80% 2-methyl-1,3 dioxolane 85% Acetic Acid  50%*1,4-dioxane 90% Acetaldehyde Not relevant

Flow 15 (partially purified process wastewater:permeate from reverseosmosis)

Mass Flow (total) 2220 kg/h Water with: ethylene glycol   0.1%2-methyl-1,3 dioxolane 0.005% Acetic Acid   0.08%* 1,4-dioxane 0.003%Acetaldehyde Not relevant Temperature 30-40° C. Discharge as wastewaterfor final purification in a chemical biological wastewater treatment.

Flow 2 (SEG from prepolycondensation)

Mass flow (total) 1375 kg/h Ethylene glycol with: water    5%2-methyl-1,3 dioxolane 0.45% Acetic Acid   0.1%* 1,4-dioxane 0.03%Acetaldehyde Not relevant Temperature 40° C.

Conditions for MDO cleavage in the SEG collecting tank (1)

Dwell time 1.5 h Temperature 45° C. Concentration of water  15%Concentration of acid 0.2% exhaust air discharge suctioning off of theacetaldehyde formed, Discharge via exhaust air collector line to thermalor catalytic exhaust air treatment Cleavage rate of MDO  50%

Flow 4 (SEG flow+retentate, after MDO cleavage at 50%)

Mass flow (total) 1555 kg/h Ethylene glycol with: Water    15%2-methyl-1,3 dioxolane   0.2% Acetic Acid     0.2% * 1,4-dioxane 0.065%Acetaldehyde Not relevant Temperature 40° C. EG recovery rate Free EGfed in addition to process column: 10.1 kg/h = 0.73 kg/t PET

The acetaldehyde formed in addition to the ethylene glycol during theMDO cleavage is largely fed via the ventilation of the SEG collectiontank via exhaust air collector line to a thermal or catalytic exhaustair purification.

EXAMPLE 2

The following tables show the material flows in a PET productionprocess, wherein in contrast to the method according to Example 1, thepartially purified process wastewater is not stripped after runningthrough the process column (5) and the condenser (6).

Flow 16 (partially purified wastewater after process column andcondenser)

Mass flow (total) 2613 kg/h Water with: Ethylene glycol  0.5%2-methyl-1,3 dioxolane 0.45% Acetic Acid  0.18%* 1,4-dioxane 0.05%Acetaldehyde Not relevant Temperature 35-45° C.

Flow 14 (partially purified process wastewater retentate from reverseosmosis)

Mass flow (total) 180 kg/h Water with: Ethylene glycol  5.8%2-methyl-1,3 dioxolane  5.5% Acetic Acid   1.3%* 1,4-dioxane 0.65%Acetaldehyde Not relevant Temperature 30-40° C.

Retention degrees according to reverse osmosis

Ethylene glycol 80% 2-methyl-1,3 dioxolane 85% Acetic Acid 50%1,4-dioxane 90% Acetaldehyde Not relevant

Flow 15 (partially purified process wastewater: permeate from reverseosmosis)

Mass flow (total) 2433 kg/h Water with: Ethylene glycol  0.1%2-methyl-1,3 dioxolane 0.07% Acetic Acid 0.095%* 1,4-dioxane 0.004% Acetaldehyde Not relevant Temperature 30-40° C. Discharge as wastewaterfor final purification in a chemical-biological wastewater treatment.

Flow 2 (SEG from prepolycondensation)

Mass flow 1375 kg/h Ethylene glycol with: Water    5% 2-methyl-1,3dioxolane 0.45% Acetic Acid  0.1% 1,4-dioxane 0.03% Acetaldehyde Notrelevant Temperature 40° C.

Conditions for MDO cleavage in the SEG collecting tank (1)

Dwell time 1.5 h Temperature 45° C. Concentration of water  15%Concentration of acid 0.2% Exhaust air discharge suctioning off of theacetaldehyde formed, Discharge via exhaust air collector line to thermalor catalytic exhaust air treatment Cleavage rate of MDO  50%

Flow 4 SEG flow+retentate after MDO cleavage at 50%)

Mass flow (total) 1555 kg/h Ethylene glycol with Water   14%2-methyl-1,3 dioxolane  0.5% Acetic Acid  0.24%* 1,4-dioxane  0.1%Acetaldehyde Not relevant Temperature 40° C. EG recovery rate-Free EGfed in addition to process column 16.2 kg/h = approx. 1.2 kg/t PET

The acetaldehyde formed in addition to the ethylene glycol during theMDO cleavage is largely fed via the ventilation of the SEG collectingtank via exhaust air collector line to a thermal or catalytic exhaustair purification.

1. An apparatus for the production of PET, the apparatus comprising: atleast one esterification or transesterification reactor; at least onerectification column downstream of the esterification ortransesterification reactor; a collecting tank arranged upstream of therectification column and downstream of the esterification ortransesterification reactor; first feed means for introducing apartially purified process wastewater containing 2-methyl-1,3-dioxolaneinto the collecting tank; second feed means for introducing spentethylene glycol from the esterification or transesterification reactorinto the collecting tank; and third feed means for channeling a mixtureof partially purified process waste water and spent ethylene glycol fromthe collecting tank to the rectification column
 2. The apparatus definedin claim 1, further comprising: a reverse osmosis orultra/nanofiltration apparatus upstream of the tank and having aretentate compartment for collecting the partially purified processwaste water for introduction into the collecting tank, a permeatecompartment for collecting additional partially purified process wastewater for removal from the process, and an osmotic membrane separatingthe retentate compartment from the permeate compartment.
 3. Theapparatus defined in claim 1 wherein the volume of the collecting tankis dimensioned such that the dwell time of the mixture containing thepartially purified process waste water and the spent ethylene glycol is0.2-4 hours.
 4. The apparatus defined in claim 1 wherein each feed meansincludes a feed conduit.